Method of manufacturing bulked continuous filaments

ABSTRACT

A method of manufacturing bulked continuous carpet filament which, in various embodiments, comprises: (A) grinding recycled PET bottles into a group of flakes; (B) washing the flakes; (C) identifying and removing impurities, including impure flakes, from the group of flakes; (D) passing the group of flakes through an MRS extruder while maintaining the pressure within the MRS portion of the MRS extruder below about 5 millibars; (E) passing the resulting polymer melt through at least one filter having a micron rating of less than about 50 microns; and (F) forming the recycled polymer into bulked continuous carpet filament that consists essentially of recycled PET.

CROSS REFERENCE TO RELATED APPLICATION

This application is a continuation of U.S. patent application Ser. No.13/892,713, filed May 13, 2013, entitled “Systems and Methods forManufacturing Bulked Continuous Filament”, which is a divisional of U.S.patent application Ser. No. 13/721,955, filed Dec. 20, 2012, entitled“Systems and Methods for Manufacturing Bulked Continuous Filament”,which claimed priority from U.S. Patent Application No. 61/654,016,filed May 31, 2012, entitled “Systems and Methods for ManufacturingBulked Continuous Fiber,” all of which are hereby incorporated herein byreference in their entirety.

BACKGROUND

Because pure virgin PET polymer is more expensive than recycled PETpolymer, and because of the environmental benefits associated with usingrecycled polymer, it would be desirable to be able to produce bulkedcontinuous carpet filament from 100% recycled PET polymer (e.g., PETpolymer from post-consumer PET bottles).

SUMMARY

A method of manufacturing bulked continuous carpet filament, accordingto particular embodiments comprises: (A) providing a multi-screwextruder; (B) using a pressure regulation system to reduce a pressurewithin the multi-screw extruder to below about 5 millibars; (C) whilemaintaining the pressure within the multi-screw extruder below about 5millibars, passing a melt comprising recycled polymer through themulti-screw extruder; and (D) after the step of passing the melt ofrecycled polymer through the multi-screw extruder, forming the recycledpolymer into bulked continuous carpet filament. In various embodiments,the multi-screw extruder comprises: (i) a first satellite screw extrudercomprising a first satellite screw that is mounted to rotate about acentral axis of the first satellite screw; (ii) a second satellite screwextruder comprising a second satellite screw that is mounted to rotateabout a central axis of the second satellite screw; and (iii) thepressure regulation system that is adapted to maintain a pressure withinthe first and second satellite screw extruders below about 5 millibars.In particular embodiments, when passing the melt comprising recycledpolymer through the multi-screw extruder: (1) a first portion of themelt passes through the first satellite screw extruder; and (2) a secondportion of the melt passes through the second satellite screw extruder.

An extruder for use in extruding a polymer melt, according to particularembodiments, comprises: (1) a first satellite screw extruder comprisinga first satellite screw that is mounted to rotate about a central axisof the first satellite screw; (2) a second satellite screw extrudercomprising a second satellite screw that is mounted to rotate about acentral axis of the second satellite screw; and (3) a pressureregulation system that is adapted to maintain a pressure within thefirst and second satellite screw extruders below a pressure of about 1.5millibars as the polymer melt passes through the first and second screwextruders.

A bulked continuous carpet filament, according to various embodiments,consists essentially of a recycled polymer.

A method of manufacturing carpet filament, according to particularembodiments, comprises the steps of: (A) washing a group of polymerflakes to remove at least a portion of one or more contaminants from asurface of the flakes, the group of flakes comprising a first pluralityof flakes that consist essentially of PET and a second plurality offlakes that do not consist essentially of PET; (B) after the step ofwashing the first plurality of flakes: (i) scanning the washed group offlakes to identify the second plurality of flakes, and (ii) separatingthesecond plurality of flakes from the first plurality of flakes; (C)melting the second plurality of flakes to produce a polymer melt; (D)providing an extruder that extrudes material in a plurality of differentextrusion streams; (E) reducing a pressure within the extruder to belowabout 5 millibars; (F) while maintaining the pressure within theextruder below about 5 millibars, passing the polymer melt through theextruder so that the polymer melt is divided into a plurality ofextrusion streams, each having a pressure below about 5 millibars; (G)after passing the polymer melt through the extruder, filtering thepolymer melt through at least one filter; and (H) after passing thepolymer melt through the filter, forming the recycled polymer intobulked continuous carpet filament.

BRIEF DESCRIPTION OF THE DRAWINGS

Having described various embodiments in general terms, reference willnow be made to the accompanying drawings, which are not necessarilydrawn to scale, and wherein:

FIG. 1 depicts a process flow, according to a particular embodiment, formanufacturing bulked continuous carpet filament.

FIG. 2 is a perspective view of an MRS extruder that is suitable for usein the process of FIG. 1.

FIG. 3 is a cross-sectional view of an exemplary MRS section of the MRSextruder of FIG. 2.

FIG. 4 depicts a process flow depicting the flow of polymer through anMRS extruder and filtration system according to a particular embodiment.

FIG. 5 is a high-level flow chart of a method, according to variousembodiments, of manufacturing bulked continuous carpet filament.

DETAILED DESCRIPTION OF VARIOUS EMBODIMENTS

Various embodiments will now be described in greater detail. It shouldbe understood that the invention may be embodied in many different formsand should not be construed as limited to the embodiments set forthherein. Rather, these embodiments are provided so that this disclosurewill be thorough and complete, and will fully convey the scope of theinvention to those skilled in the art. Like numbers refer to likeelements throughout.

I. Overview

New processes for making fiber from recycled polymer (e.g., recycled PETpolymer) are described below. In various embodiments, this new process:(1) is more effective than earlier processes in removing contaminatesand water from the recycled polymer; and/or (2) does not require thepolymer to be melted and cooled as many times as in earlier processes.In at least one embodiment, the improved process results in a recycledPET polymer having a polymer quality that is high enough that the PETpolymer may be used in producing bulked continuous carpet filament from100% recycled PET content (e.g., 100% from PET obtained from previouslyused PET bottles). In particular embodiments, the recycled PET polymerhas an intrinsic viscosity of at least about 0.79 dL/g (e.g., of betweenabout 0.79 dL/g and about 1.00 dL/g).

II. More Detailed Discussion

A BCF (bulked continuous filament) manufacturing process, according to aparticular embodiment, may generally be broken down into three steps:(1) preparing flakes of PET polymer from post-consumer bottles for usein the process; (2) passing the flakes through an extruder that meltsthe flakes and purifies the resulting PET polymer; and (3) feeding thepurified polymer into a spinning machine that turns the polymer intofilament for use in manufacturing carpets. These three steps aredescribed in greater detail below.

STEP 1: Preparing Flakes of PET Polymer from Post-Consumer Bottles

In a particular embodiment, the step of preparing flakes of PET polymerfrom post-consumer bottles comprises: (A) sorting post-consumer PETbottles and grinding the bottles into flakes; (B) washing the flakes;and (C) identifying and removing any impurities or impure flakes.

A. Sorting Post-Consumer PET bottles and Grinding the Bottles intoFlakes

In particular embodiments, bales of clear and mixed colored recycledpost-consumer (e.g., “curbside”) PET bottles (or other containers)obtained from various recycling facilities make-up the post-consumer PETcontainers for use in the process. In other embodiments, the source ofthe post-consumer PET containers may be returned ‘deposit’ bottles(e.g., PET bottles whose price includes a deposit that is returned to acustomer when the customer returns the bottle after consuming thebottle's contents). The curbside or returned “post-consumer” or“recycled” containers may contain a small level of non-PET contaminates.The contaminants in the containers may include, for example, non-PETpolymeric contaminants (e.g., PVC, PLA, PP, PE, PS, PA, etc.), metal(e.g., ferrous and non-ferrous metal), paper, cardboard, sand, glass orother unwanted materials that may find their way into the collection ofrecycled PET. The non-PET contaminants may be removed from the desiredPET components, for example, through one or more of the variousprocesses described below.

In particular embodiments, smaller components and debris (e.g.,components and debris greater than 2 inches in size) are removed fromthe whole bottles via a rotating trammel. Various metal removal magnetsand eddy current systems may be incorporated into the process to removeany metal contaminants. Near Infra-Red optical sorting equipment such asthe NRT Multi Sort IR machine from Bulk Handling Systems Company ofEugene, Oregon, or the Spyder IR machine from National RecoveryTechnologies of Nashville, Tennessee, may be utilized to remove anyloose polymeric contaminants that may be mixed in with the PET flakes(e.g., PVC, PLA, PP, PE, PS, and PA). Additionally, automated X-raysorting equipment such as a VINYLCYCLE machine from National RecoveryTechnologies of Nashville, Tennessee may be utilized to remove remainingPVC contaminants.

In particular embodiments, a binary segregation of the clear materialsfrom the colored materials is achieved using automated color sortingequipment equipped with a camera detection system (e.g., an Multisort ESmachine from National Recovery Technologies of Nashville, Tenn.). Invarious embodiments, manual sorters are stationed at various points onthe line to remove contaminants not removed by the sorter and anycolored bottles. In particular embodiments, the sorted material is takenthrough a granulation step (e.g., using a 50 B Granulator machine fromCumberland Engineering Corporation of New Berlin, Wisconsin) to sizereduce (e.g., grind) the bottles down to a size of less than one half ofan inch. In various embodiments, the bottle labels are removed from theresultant “dirty flake” (e.g., the PET flakes formed during thegranulation step) via an air separation system prior to entering thewash process.

B. Washing the Flakes

In particular embodiments, the “dirty flake” is then mixed into a seriesof wash tanks As part of the wash process, in various embodiments, anaqueous density separation is utilized to separate the olefin bottlecaps (which may, for example, be present in the “dirty flake” asremnants from recycled PET bottles) from the higher specific gravity PETflakes. In particular embodiments, the flakes are washed in a heatedcaustic bath to about 190 degrees Fahrenheit. In particular embodiments,the caustic bath is maintained at a concentration of between about 0.6%and about 1.2% sodium hydroxide. In various embodiments, soapsurfactants as well as defoaming agents are added to the caustic bath,for example, to further increase the separation and cleaning of theflakes. A double rinse system then washes the caustic from the flakes.

In various embodiments, the flake is centrifugally dewatered and thendried with hot air to at least substantially remove any surfacemoisture. The resultant “clean flake” is then processed through anelectrostatic separation system (e.g., an electrostatic separator fromCarpco, Inc. of Jacksonville, Florida) and a flake metal detectionsystem (e.g., an MSS Metal Sorting System) to further remove any metalcontaminants that remain in the flake. In particular embodiments, an airseparation step removes any remaining label from the clean flake. Invarious embodiments, the flake is then taken through a flake colorsorting step (e.g., using an OPTIMIX machine from TSM Control Systems ofDundalk, Ireland) to remove any remaining color contaminants remainingin the flake. In various embodiments, an electro-optical flake sorterbased at least in part on Raman technology (e.g., a Powersort 200 fromUnisensor Sensorsysteme GmbH of Karlsruhe, Germany) performs the finalpolymer separation to remove any non-PET polymers remaining in theflake. This step may also further remove any remaining metalcontaminants and color contaminants.

In various embodiments, the combination of these steps deliverssubstantially clean (e.g., clean) PET bottle flake comprising less thanabout 50 parts per million PVC (e.g., 25 ppm PVC) and less than about 15parts per million metals for use in the downstream extrusion processdescribed below.

C. Identifying and Removing Impurities and Impure Flakes

In particular embodiments, after the flakes are washed, they are feddown a conveyor and scanned with a high-speed laser system 300. Invarious embodiments, particular lasers that make up the high-speed lasersystem 300 are configured to detect the presence of particularcontaminates (e.g., PVC or Aluminum). Flakes that are identified as notconsisting essentially of PET may be blown from the main stream offlakes with air jets. In various embodiments, the resulting level ofnon-PET flakes is less than 25 ppm.

In various embodiments, the system is adapted to ensure that the PETpolymer being processed into filament is substantially free of water(e.g., entirely free of water). In a particular embodiment, the flakesare placed into a pre-conditioner for between about 20 and about 40minutes (e.g., about 30 minutes) during which the pre-conditioner blowsthe surface water off of the flakes. In particular embodiments,interstitial water remains within the flakes. In various embodiments,these “wet” flakes (e.g., flakes comprising interstitial water) may thenbe fed into an extruder (e.g., as described in Step 2 below), whichincludes a vacuum setup designed to remove—among other things—theinterstitial water that remains present in the flakes following thequick-drying process described above.

STEP 2: Using an Extrusion System to Melt and Purify PET Flakes

In particular embodiments, an extruder is used to turn the wet flakesdescribed above into a molten recycled PET polymer and to perform anumber of purification processes to prepare the polymer to be turnedinto BCF for carpet. As noted above, in various embodiments, after STEP1 is complete, the recycled PET polymer flakes are wet (e.g., surfacewater is substantially removed (e.g., fully removed) from the flakes,but interstitial water remains in the flakes). In particularembodiments, these wet flakes are fed into a Multiple Rotating Screw(“MRS”) extruder 400. In other embodiments, the wet flakes are fed intoany other suitable extruder (e.g., a twin screw extruder, a multiplescrew extruder, a planetary extruder, or any other suitable extrusionsystem). An exemplary MRS Extruder 400 is shown in FIGS. 2 and 3. Aparticular example of such an MRS extruder is described in U.S.Published Patent Application 2005/0047267, entitled “Extruder forProducing Molten Plastic Materials”, which was published on Mar. 3,2005, and which is hereby incorporated herein by reference.

As may be understood from this figure, in particular embodiments, theMRS extruder includes a first single-screw extruder section 410 forfeeding material into an MRS section 420 and a second single-screwextruder section 440 for transporting material away from the MRSsection.

In various embodiments, the wet flakes are fed directly into the MRSextruder 400 substantially immediately (e.g., immediately) following thewashing step described above (e.g., without drying the flakes orallowing the flakes to dry). In particular embodiments, a system thatfeeds the wet flakes directly into the MRS Extruder 400 substantiallyimmediately (e.g., immediately) following the washing step describedabove may consume about 20% less energy than a system that substantiallyfully pre-dries the flakes before extrusion (e.g., a system thatpre-dries the flakes by passing hot air over the wet flakes for aprolonged period of time). In various embodiments, a system that feedsthe wet flakes directly into the MRS Extruder 400 substantiallyimmediately (e.g., immediately) following the washing step describedabove avoids the need to wait a period of time (e.g., up to eight hours)generally required to fully dry the flakes (e.g., remove all of thesurface and interstitial water from the flakes).

FIG. 4 depicts a process flow that illustrates the various processesperformed by the MRS Extruder 400 in a particular embodiment. In theembodiment shown in this figure, the wet flakes are first fed throughthe MRS extruder's first single-screw extruder section 410, which may,for example, generate sufficient heat (e.g., via shearing) to at leastsubstantially melt (e.g., melt) the wet flakes.

The resultant polymer melt (e.g., comprising the melted flakes), invarious embodiments, is then fed into the extruder's MRS section 420, inwhich the extruder separates the melt flow into a plurality of differentstreams (e.g., 4, 6, 8, or more streams) through a plurality of openchambers. FIG. 3 shows a detailed cutaway view of an MRS Section 420according to a particular embodiment. In particular embodiments, such asthe embodiment shown in this figure, the MRS Section 420 separates themelt flow into eight different streams, which are subsequently fedthrough eight satellite screws 425A-H. As may be understood from FIG. 2,in particular embodiments, these satellite screws are substantiallyparallel (e.g., parallel) to one other and to a primary screw axis ofthe MRS Machine 400.

In the MRS section 420, in various embodiments, the satellite screws425A-H may, for example, rotate faster than (e.g., about four timesfaster than) in previous systems. As shown in FIG. 3, in particularembodiments: (1) the satellite screws 425A-H are arranged within asingle screw drum 428 that is mounted to rotate about its central axis;and (2) the satellite screws 425A-H are configured to rotate in adirection that is opposite to the direction in which the single screwdrum rotates 428. In various other embodiments, the satellite screws425A-H and the single screw drum 428 rotate in the same direction. Inparticular embodiments, the rotation of the satellite screws 425A-H isdriven by a ring gear. Also, in various embodiments, the single screwdrum 428 rotates about four times faster than each individual satellitescrew 425A-H. In certain embodiments, the satellite screws 425A-H rotateat substantially similar (e.g., the same) speeds.

In various embodiments, as may be understood from FIG. 4, the satellitescrews 425A-H are housed within respective extruder barrels, which may,for example be about 30% open to the outer chamber of the MRS section420. In particular embodiments, the rotation of the satellite screws425A-H and single screw drum 428 increases the surface exchange of thepolymer melt (e.g., exposes more surface area of the melted polymer tothe open chamber than in previous systems). In various embodiments, theMRS section 420 creates a melt surface area that is, for example,between about twenty and about thirty times greater than the meltsurface area created by a co-rotating twin screw extruder. In aparticular embodiment, the MRS section 420 creates a melt surface areathat is, for example, about twenty five times greater than the meltsurface area created by a co-rotating twin screw extruder

In various embodiments, the MRS extruder's MRS Section 420 is fittedwith a Vacuum Pump 430 that is attached to a vacuum attachment portion422 of the MRS section 420 so that the Vacuum Pump 430 is incommunication with the interior of the MRS section via a suitableopening 424 in the MRS section's housing. In still other embodiments,the MRS Section 420 is fitted with a series of Vacuum Pumps. Inparticular embodiments, the Vacuum Pump 430 is configured to reduce thepressure within the interior of the MRS Section 420 to a pressure thatis between about 0.5 millibars and about 5 millibars. In particularembodiments, the Vacuum Pump 430 is configured to reduce the pressure inthe MRS Section 420 to less than about 1.5 millibars (e.g., about 1millibar or less). The low-pressure vacuum created by the Vacuum Pump430 in the MRS Section 420 may remove, for example: (1) volatileorganics present in the melted polymer as the melted polymer passesthrough the MRS Section 420; and/or (2) at least a portion of anyinterstitial water that was present in the wet flakes when the wetflakes entered the MRS Extruder 400. In various embodiments, thelow-pressure vacuum removes substantially all (e.g., all) of the waterand contaminants from the polymer stream.

In a particular example, the Vacuum Pump 430 comprises three mechanicallobe vacuum pumps (e.g., arranged in series) to reduce the pressure inthe chamber to a suitable level (e.g., to a pressure of about 1.0millibar). In other embodiments, rather than the three mechanical lobevacuum pump arrangement discussed above, the Vacuum Pump 430 includes ajet vacuum pump fit to the MRS extruder. In various embodiments, the jetvacuum pump is configured to achieve about 1 millibar of pressure in theinterior of the MRS section 420 and about the same results describedabove regarding a resulting intrinsic viscosity of the polymer melt. Invarious embodiments, using a jet vacuum pump can be advantageous becausejet vacuum pumps are steam powered and therefore substantiallyself-cleaning (e.g., self-cleaning), thereby reducing the maintenancerequired in comparison to mechanical lobe pumps (which may, for example,require repeated cleaning due to volatiles coming off and condensing onthe lobes of the pump). In a particular embodiment, the Vacuum Pump 430is a jet vacuum pump is made by Arpuma GmbH of Bergheim, Germany.

In particular embodiments, after the molten polymer is run the throughthe multi-stream MRS Section 420, the streams of molten polymer arerecombined and flow into the MRS extruder's second single screw section440. In various embodiments, the single stream of molten polymer is nextrun through a filtration system 450 that includes at least one filter.In a particular embodiment, the filtration system 450 includes twolevels of filtration (e.g., a 40 micron screen filter followed by a 25micron screen filter). Although, in various embodiments, water andvolatile organic impurities are removed during the vacuum process asdiscussed above, particulate contaminates such as, for example, aluminumparticles, sand, dirt, and other contaminants may remain in the polymermelt. Thus, this filtration step may be advantageous in removingparticulate contaminates (e.g., particulate contaminates that were notremoved in the MRS Section 420).

In particular embodiments, a viscosity sensor 460 (see FIG. 4) is usedto sense the melt viscosity of the molten polymer stream following itspassage through the filtration system 450. In various embodiments, theviscosity sensor 460, measures the melt viscosity of the stream, forexample, by measuring the stream's pressure drop across a known area. Inparticular embodiments, in response to measuring an intrinsic viscosityof the stream that is below a predetermined level (e.g., below about 0.8g/dL), the system may: (1) discard the portion of the stream with lowintrinsic viscosity; and/or (2) lower the pressure in the MRS Section420 in order to achieve a higher intrinsic viscosity in the polymermelt. In particular embodiments, decreasing the pressure in the MRSSection 420 is executed in a substantially automated manner (e.g.,automatically) using the viscosity sensor in a computer-controlledfeedback control loop with the vacuum section 430.

In particular embodiments, removing the water and contaminates from thepolymer improves the intrinsic viscosity of the recycled PET polymer byallowing polymer chains in the polymer to reconnect and extend the chainlength. In particular embodiments, following its passage through the MRSSection 420 with its attached Vacuum Pump 430, the recycled polymer melthas an intrinsic viscosity of at least about 0.79 dL/g (e.g., of betweenabout 0.79 dL/g and about 1.00 dL/g). In particular embodiments, passagethrough the low pressure MRS Section 420 purifies the recycled polymermelt (e.g., by removing the contaminants and interstitial water) andmakes the recycled polymer substantially structurally similar to (e.g.,structurally the same as) pure virgin PET polymer. In particularembodiments, the water removed by the vacuum includes both water fromthe wash water used to clean the recycled PET bottles as describedabove, as well as from unreacted water generated by the melting of thePET polymer in the single screw heater 410 (e.g., interstitial water).In particular embodiments, the majority of water present in the polymeris wash water, but some percentage may be unreacted water.

In particular embodiments, the resulting polymer is a recycled PETpolymer (e.g., obtained 100% from post-consumer PET products, such asPET bottles or containers) having a polymer quality that is suitable foruse in producing PET carpet filament using substantially only (e.g.,only) PET from recycled PET products.

Step 3: Purified PET Polymer Fed into Spinning Machine to be Turned intoCarpet Yarn

In particular embodiments, after the recycled PET polymer has beenextruded and purified by the above-described extrusion process, theresulting molten recycled PET polymer is fed directly into a BCF (or“spinning”) machine 500 that is configured to turn the molten polymerinto bulked continuous filament. For example, in various embodiments,the output of the MRS extruder 400 is connected substantially directly(e.g., directly) to the input of the spinning machine 500 so that moltenpolymer from the extruder is fed directly into the spinning machine 500.This process may be advantageous because molten polymer may, in certainembodiments, not need to be cooled into pellets after extrusion (as itwould need to be if the recycled polymer were being mixed with virginPET polymer). In particular embodiments, not cooling the recycled moltenpolymer into pellets serves to avoid potential chain scission in thepolymer that might lower the polymer's intrinsic viscosity.

In particular embodiments, the spinning machine 500 extrudes moltenpolymer through small holes in a spinneret in order to produce carpetyarn filament from the polymer. In particular embodiments, the moltenrecycled PET polymer cools after leaving the spinneret. The carpet yarnis then taken up by rollers and ultimately turned into filaments thatare used to produce carpet. In various embodiments, the carpet yarnproduced by the spinning machine 500 may have a tenacity between about 3gram-force per unit denier (gf/den) and about 9 gf/den. In particularembodiments, the resulting carpet yarn has a tenacity of at least about3 gf/den.

In particular embodiments, the spinning machine 500 used in the processdescribed above is the Sytec One spinning machine manufactured byOerlika Neumag of Neumuenster, Germany. The Sytec One machine may beespecially adapted for hard-to-run fibers, such as nylon orsolution-dyed fibers, where the filaments are prone to breakage duringprocessing. In various embodiments, the Sytec One machine keeps the runsdownstream of the spinneret as straight as possible, uses only onethreadline, and is designed to be quick to rethread when there arefilament breaks.

Although the example described above describes using the Sytec Onespinning machine to produce carpet yarn filament from the polymer, itshould be understood that any other suitable spinning machine may beused. Such spinning machines may include, for example, any suitableone-threadline or three-threadline spinning machine made by OerlikaNeumag of Neumuenster, Germany or any other company.

In various embodiments, the improved strength of the recycled PETpolymer generated using the process above allows it to be run at higherspeeds through the spinning machine 500 than would be possible usingpure virgin PET polymer. This may allow for higher processing speedsthan are possible when using virgin PET polymer.

Summary of Exemplary Process

FIG. 5 provides a high-level summary of the method of manufacturingbulked continuous filament described above. As shown in the figure, themethod begins at Step 602, where recycled PET bottles are ground into agroup of flakes. Next, at Step 604, the group of flakes is washed toremove contaminants from the flakes' respective outer surfaces. Next, atStep 606, the group of flakes is scanned (e.g., using one or more of themethods discussed above) to identify impurities, including impureflakes. These impurities, and impure flakes, are then removed from thegroup of flakes.

Next, at Step 608, the group of flakes is passed through an MRS extruderwhile maintaining the pressure within an MRS portion of the extruderbelow about 1.5 millibars. At Step 610, the resulting polymer melt ispassed through at least one filter having a micron rating of less thanabout 50 microns. Finally, at Step 612, the recycled polymer is formedinto bulked continuous carpet filament, which may be used in producingcarpet. The method then ends at Step 614.

Alternative Embodiments

In particular embodiments, the system may comprise alternativecomponents or perform alternative processes in order to producesubstantially continuous BCF from 100% recycled PET, or other recycledpolymer. Exemplary alternatives are discussed below.

Non-MRS Extrusion System

In particular embodiments, the process may utilize a polymer flowextrusion system other than the MRS Extruder described above. Thealternative extrusion system may include for example, a twin screwextruder, a multiple screw extruder, a planetary extruder, or any othersuitable extrusion system. In a particular embodiment, the process mayinclude a plurality of any combination of any suitable conical screwextruders (e.g., four twin screw extruders, three multiple screwextruders, etc.).

Making Carpet Yarn from 100% Recycled Carpet

In particular embodiments, the process described above may be adaptedfor processing and preparing old carpet (or any other suitablepost-consumer product) to produce new carpet yarn comprising 100%recycled carpet. In such embodiments, the process would begin bygrinding and washing recycled carpet rather than recycled PET bottles.In various embodiments where old carpet is converted into new carpetyarn comprising 100% recycled carpet, the process may compriseadditional steps to remove additional materials or impurities that maybe present in recycled carpet that may not be present in recycled PETbottles (e.g., carpet backing, adhesive, etc.).

Other Sources of Recycled PET

In various embodiments, the process described above is adapted forprocessing recycled PET from any suitable source (e.g., sources otherthan recycled bottles or carpet) to produce new carpet yarn comprising100% recycled PET.

CONCLUSION

Many modifications and other embodiments of the invention will come tomind to one skilled in the art to which this invention pertains havingthe benefit of the teachings presented in the foregoing descriptions andthe associated drawings. For example, although the vacuum systemdiscussed above is described as being configured to maintain thepressure in the open chambers of the MRS extruder to about 1 mbar, inother embodiments, the vacuum system may be adapted to maintain thepressure in the open chambers of the MRS extruder at pressures greaterthan, or less than, 1 mbar. For example, the vacuum system may beadapted to maintain this pressure at between about 0.5 mbar and about1.2 mbar.

Similarly, although various embodiments of the systems described abovemay be adapted to produce carpet filament from substantially onlyrecycled PET (so the resulting carpet filament would comprise, consistof, and/or consist essentially of recycled PET), in other embodiments,the system may be adapted to produce carpet filament from a combinationof recycled PET and virgin PET. The resulting carpet filament may, forexample, comprise, consist of, and/or consist essentially of betweenabout 80% and about 100% recycled PET, and between about 0% and about20% virgin PET.

Also, while various embodiments are discussed above in regard toproducing carpet filament from PET, similar techniques may be used toproduce carpet filament from other polymers. Similarly, while variousembodiments are discussed above in regard to producing carpet filamentfrom PET, similar techniques may be used to produce other products fromPET or other polymers.

In addition, it should be understood that various embodiments may omitany of the steps described above or add additional steps.

In light of the above, it is to be understood that the invention is notto be limited to the specific embodiments disclosed and thatmodifications and other embodiments are intended to be included withinthe scope of the appended claims. Although specific terms are employedherein, they are used in a generic and descriptive sense only and notfor the purposes of limitation.

I claim:
 1. A method of manufacturing bulked continuous carpet filament,said method comprising: (A) providing a multi-screw extruder thatcomprises: (i) a first satellite screw extruder, said first satellitescrew extruder comprising a first satellite screw that is mounted torotate about a central axis of said first satellite screw; (ii) a secondsatellite screw extruder, said second satellite screw extrudercomprising a second satellite screw that is mounted to rotate about acentral axis of said second satellite screw; (iii) a third satellitescrew extruder, said third satellite screw extruder comprising a thirdsatellite screw that is mounted to rotate about a central axis of saidthird satellite screw; (iv) a fourth satellite screw extruder, saidfourth satellite screw extruder comprising a fourth satellite screw thatis mounted to rotate about a central axis of said fourth satellitescrew; and (v) a pressure regulation system that is adapted to maintaina pressure within said first, second, third, and fourth satellite screwextruders between about 0 millibars and about 5 millibars; (B) usingsaid pressure regulation system to reduce a pressure within said first,second, third, and fourth satellite screw extruders to between about 0millibars and about 5 millibars; (C) while maintaining said pressurewithin said first, second, third, and fourth satellite screw extrudersbetween about 0 millibars and about 5 millibars, passing a meltcomprising recycled polymer through said multi-screw extruder so that:(1) a first portion of said melt passes through said first satellitescrew extruder, (2) a second portion of said melt passes through saidsecond satellite screw extruder, (3) a third portion of said melt passesthrough said third satellite screw extruder, and (4) a fourth portion ofsaid melt passes through said fourth satellite screw extruder; and (D)after said step of passing said melt of recycled polymer through saidmulti-screw extruder, forming said recycled polymer into bulkedcontinuous carpet filament.
 2. The method of claim 1, wherein saidmulti-screw extruder comprises a satellite screw extruder support systemthat is adapted to rotate said first, second, third, and fourthsatellite screws about a main axis, said main axis being substantiallyparallel to: (a) said central axis of said first satellite screw; (b)said central axis of said second satellite screw; (c) said central axisof said third satellite screw; and (d) said central axis of said fourthsatellite screw.
 3. The method of claim 2, wherein said step of passingsaid melt of recycled polymer through said multi-screw extruder occurswhile said first, second, third, and fourth satellite screw extrudersare orbitally rotating about said main axis.
 4. The method of claim 1,wherein said recycled polymer consists essentially of recycledpolyethylene terephthalate.
 5. The method of claim 4, wherein saidpressure regulation system comprises a jet vacuum pump.
 6. The method ofclaim 2, wherein: said satellite screw extruder support system comprisesa drum that is adapted to rotate about said main axis; said drum definesa first screw barrel having a central axis that is substantiallyparallel to said main axis; said drum defines a second screw barrelhaving a central axis that is substantially parallel to said main axis;said drum defines a third screw barrel having a central axis that issubstantially parallel to said main axis; said drum defines a fourthscrew barrel having a central axis that is substantially parallel tosaid main axis; said first satellite screw is rotatably mounted withinsaid first screw barrel; said second satellite screw is rotatablymounted within said second screw barrel; said third satellite screw isrotatably mounted within said third screw barrel; and said fourthsatellite screw is rotatably mounted within said fourth screw barrel. 7.The method of claim 1, wherein: said extruder is a first extruder; andsaid method further comprises: passing a plurality of flakes of recycledPET through a second extruder; and while passing said plurality offlakes through said second extruder, using said second extruder to heatsaid plurality of flakes to a temperature that is sufficient to at leastsubstantially melt said plurality of flakes to form said polymer melt.8. The method of claim 7, wherein said method further comprises: beforesaid step of passing said plurality of flakes through said secondextruder: washing said plurality of flakes; scanning said washedplurality of flakes to identify any of said plurality of flakes thatcomprise material other than PET; and removing at least one of saididentified flakes that comprise material other than PET.
 9. The methodof claim 1, wherein, after said step of passing said melt of recycledpolymer through said multi-screw extruder, said polymer melt has anintrinsic viscosity of between about 0.79 dL/g and about 1.00 dL/g. 10.The method of claim 1, further comprising, after said step of passingsaid melt of recycled polymer through said multi-screw extruder, passingsaid polymer melt though at least one filter having a micron rating ofless than about 25 microns.
 11. The method of claim 1, wherein said stepof forming said recycled polymer into bulked continuous carpet filamentcomprises spinning said polymer melt to form said bulked continuouscarpet filament.
 12. The method of claim 1, further comprising, beforesaid step of forming said recycled polymer into bulked continuous carpetfilament: using a viscosity sensor to determine whether an intrinsicviscosity of at least a portion of recycled polymer is within apre-determined range; and in response to determining said intrinsicviscosity is not within a predetermined range, adjusting said pressureregulation system to lower said internal pressure of said extruder. 13.A method of manufacturing bulked continuous carpet filament, said methodcomprising: (A) providing a multi-screw extruder that comprises: atleast six satellite screw extruders, wherein each of said at least sixsatellite screw extruders comprise a satellite screw mounted to rotateabout a respective central axis of each of said at least six satellitescrew extruders; and a pressure regulation system that is adapted tomaintain a pressure within said at least six satellite screw extrudersbetween about 0 millibars and about 5 millibars; (B) using said pressureregulation system to reduce a pressure within said at least sixsatellite screw extruders to between about 0 millibars and about 5millibars; (C) while maintaining said pressure within said at least sixsatellite screw extruders between about 0 millibars and about 5millibars, passing a melt comprising recycled polymer through saidmulti-screw extruder so that at least a portion of said melt passesthrough each of said at least six satellite screw extruders; (D) aftersaid step of passing said melt of recycled polymer through saidmulti-screw extruder, forming said recycled polymer into bulkedcontinuous carpet filament.
 14. The method of claim 13, wherein saidmulti-screw extruder comprises a satellite screw extruder support systemthat is adapted to rotate said at least six satellite screw extrudersabout a main axis that is substantially parallel to each said respectivecentral axis of each of said at least six satellite screw extruders. 15.The method of claim 14, wherein said step of passing said melt ofrecycled polymer though said multi-screw extruder occurs while said atleast six satellite screw extruders are orbitally rotating about saidmain axis.
 16. The method of claim 15, wherein said pressure regulationsystem comprises a jet vacuum pump.
 17. A method of manufacturing carpetfilament comprising the steps of: (A) washing a group of polymer flakesto remove at least a portion of one or more contaminants from a surfaceof said flakes, said group of flakes comprising a first plurality offlakes that consist essentially of PET and a second plurality of flakesthat do not consist essentially of PET; (B) after said step of washingsaid first plurality of flakes: (i) scanning said washed group of flakesto identify said second plurality of flakes, (ii) separating said secondplurality of flakes from said first plurality of flakes; (C) afterseparating said second plurality of flakes from said first plurality offlakes, melting said second plurality of flakes to produce a polymermelt; (D) providing an extruder that extrudes material in a plurality ofdifferent extrusion streams; (E) reducing a pressure within saidextruder to between about 0 millibars and about 5 millibars; (F) whilemaintaining said pressure within said extruder between about 0 millibarsand about 5 millibars, passing said polymer melt through said extruderso that said polymer melt is divided into a plurality of extrusionstreams, each having a pressure between about 0 millibars and about 5millibars; (G) after passing said polymer melt through said extruder,filtering said polymer melt through at least one filter; and (H) afterpassing said polymer melt through said filter, forming said recycledpolymer into bulked continuous carpet filament.
 18. The method of claim17, wherein said extruder comprises: (A) a first satellite screwextruder, said first satellite screw extruder comprising a firstsatellite screw that is mounted to rotate about a central axis of saidfirst satellite screw; (B) a second satellite screw extruder, saidsecond satellite screw extruder comprising a second satellite screw thatis mounted to rotate about a central axis of said second satellitescrew; (C) a pressure regulation system that is adapted to maintain apressure within said first and second satellite screw extruders betweena pressure of about 0 millibars and about 5 millibars as said polymermelt passes through said first and second screw extruders; and (D) asatellite screw extruder support system that is adapted to orbitallyrotate said first and second satellite screws about a main axis as saidpolymer melt passes through said first and second screw extruders, saidmain axis being substantially parallel to both: (1) said central axis ofsaid first satellite screw; and (2) said central axis of said secondsatellite screw.
 19. The method of claim 18, wherein: said extrudercomprises: (A) a third satellite screw extruder, said third satellitescrew extruder comprising a third satellite screw that is mounted torotate about a central axis of said third satellite screw; and (B) afourth satellite screw extruder, said fourth satellite screw extrudercomprising a fourth satellite screw that is mounted to rotate about acentral axis of said fourth satellite screw; said pressure regulationsystem is further adapted to maintain a pressure within said third andfourth satellite screw extruders between a pressure of about 0 millibarsand about 5 millibars as said polymer melt passes through said third andfourth extruders; and said satellite screw extruder support system isfurther adapted to orbitally rotate said third and fourth satellitescrews about said main axis as said polymer melt passes through saidthird and fourth screw extruders.
 20. The method of claim 19, whereinsaid at least one filter comprises: a first filter having a micronrating of less than about 50 microns; and a second filter having amicron rating of less than about 30 microns.